CN1045137A - Controlling polymers method of viscosity and equipment - Google Patents
Controlling polymers method of viscosity and equipment Download PDFInfo
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- CN1045137A CN1045137A CN90100682A CN90100682A CN1045137A CN 1045137 A CN1045137 A CN 1045137A CN 90100682 A CN90100682 A CN 90100682A CN 90100682 A CN90100682 A CN 90100682A CN 1045137 A CN1045137 A CN 1045137A
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- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01D—MECHANICAL METHODS OR APPARATUS IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS
- D01D5/00—Formation of filaments, threads, or the like
- D01D5/08—Melt spinning methods
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- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01D—MECHANICAL METHODS OR APPARATUS IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS
- D01D1/00—Treatment of filament-forming or like material
- D01D1/04—Melting filament-forming substances
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- D—TEXTILES; PAPER
- D01—NATURAL OR MAN-MADE THREADS OR FIBRES; SPINNING
- D01F—CHEMICAL FEATURES IN THE MANUFACTURE OF ARTIFICIAL FILAMENTS, THREADS, FIBRES, BRISTLES OR RIBBONS; APPARATUS SPECIALLY ADAPTED FOR THE MANUFACTURE OF CARBON FILAMENTS
- D01F6/00—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof
- D01F6/58—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolycondensation products
- D01F6/60—Monocomponent artificial filaments or the like of synthetic polymers; Manufacture thereof from homopolycondensation products from polyamides
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Abstract
By with continuous first kind of nitrogen current with variable temperature and moisture content, and second kind of drying but nitrogen current with variable flow rate is handled the uniformity of improving spun polyamide fiber silk performance to the thin slice polyamide.Determine viscosity by measuring differential pressure between the delivery catheter two ends from the molten polyamide of thin slice melter.By automaton measure the flow rate of control second air-flow with viscosity and be added to the moisture percentage of supplemental air flow in first air-flow, the flow rate of control supplemental air flow remains within the limit value second air-flow, and the temperature of controlling first air-flow makes and replenishes and the flow rate of second air-flow remains within the limit value.
Description
The present invention relates to stand the control that the viscosity of the melt polymer of depolymerization one polymerization equilibrium reaction is carried out to influenced by the melt moisture content.This control is applied in the device for spinning and technical process of polyamide especially.
When melt spinning was heated to desired temperature, polyamide can be subjected to depolymerization.The equalization point of degree of depolymerizaton or depolymerization one polymerization is the function of moisture in the melt.Sheet of nylon or other solid-state nylon raw materials as melt spinning contain different humidity according to its preprocessing and storage process.For example, the moisture that absorbs in the solid-state nylon material depends on the atmospheric humidity in the place that nylon once was exposed.The various different molecular weights of the melt polymer that is caused by the depolymerization of nylon can produce undesirable variation at aspects such as filametntary toughness, percentage elongation and dyeabilities.
As United States Patent (USP) the 2nd, 571, No. 975 and the 2nd, 943, in the prior art of being implemented in No. 350, disclose molten state or laminar nylon by a container, made nylon be exposed to steam or have in the controlled atmosphere of constant and predetermined water vapour content, with the difference of humidity in the reduction polymer and more uniform performance is provided in spun filament.Steam generally causes the excessive depolymerization of melt polymer, and laminar polymer short burst is exposed in the atmosphere of fixing humidity, generally to the water ratio uniformity aspect being provided, especially being not enough in the centre of solid-state sheet.Described polymer flake is different from the core of each thin slice to its its moisture of surface.
Device for spinning as the illustrated prior art of Fig. 1-4, this device has the automatic control system that is used for controlling the polymer relative viscosity that is carried out spinning, it comprises: totally by an adjuster of 20 expressions, this adjuster is regulated polyamide thin slice 22, in a screw melter 24, this thin slice is melted then, and be sent to manifold 28 by delivery catheter 26.Measuring pump 29 will be delivered to some spinning heads 30 from the polymer of manifold 28, and each spinning head produces many long fibers that cool off 32 in air.Automatic numerical control device controlled adjuster 20 totally by 40 expressions, so that regulate the moisture content of polyamide thin slice in the variation aspect the relative viscosity of melt polymer, thereby the relative viscosity of melt polymer is remained within the narrow range with detect.With the measurement facilities of 42 expressions relative viscosity is calculated in the handling capacity measurement of melt polymer from differential pressure, temperature and by stack up the delivery catheter 26, thereby can promptly onlinely be determined and the relative viscosity of controlling polymers.Maintain predetermined relative viscosity and produced uniformity aspect toughness, percentage elongation and the dyeability of spun filament 32 basically.
In adjuster 20, by make polymer flake by upper area or container 44, make described thin slice be exposed to circulated inert gas stream 46, make it again then by lower area or container 48, make it to be exposed to conversion inert gas stream 50 and the moisture content of telomerized polymer thin slice.Recycle gas stream 46 can regulated aspect its temperature and humidity two selectively, and this humidity is regulated successively by the flow rate that adjusting is added to the supplemental air flow 52 in the circulating current 46 again.In this prior art system, make the moisture content of supplemental air flow 52 remain on a certain predetermined value.50 of dry converted gas are regulated selectively to its flow rate.
Usually, the moisture content of polymer flake that enters adjuster 20 is greater than the moisture content that produces the relative viscosity that requires in the polymer of fusing, thereby get rid of the part moisture that is absorbed in the polymer by recyclegas 46 and converted gas 50, reach desired relative viscosity and make in the polymer of fusing.The adjusting of converted gas 50 flow rates is provided the initial control of melt polymer relative viscosity according to the detected variation aspect the relative viscosity in melt polymer.Thereby provide secondary control that the channel gas flow rate is remained in the effective working range by adjusting to the make-up gas flow rate.Being adjusted in reaction in three kinds of adjustings of polymer viscosity of recyclegas temperature is the slowest, and converted gas flow rate and make-up gas flow rate are remained within the respective range.
The vapour content percentage by weight generally is lower than the make-up gas stream 52 of recycle gas stream 46, putting 68 from air blast 62 upstreams is added in the recycle gas stream, guaranteeing the humidity regulation of recycle gas stream 46, and for providing make-up gas via the humid gas of exhaust outlet 67 outflows with via any gas of thin slice feeder system loss.Valve 69 in the control exhaust stream 67 is slightly higher than atmospheric predetermined pressure in container 44 and the recyclegas loop 46 to maintain.Fines recirculation, processing or other purposes that centrifuge 71 is got rid of from exhaust stream.Valve 72 is being controlled the flow rate from the make-up gas of dry nitrogenous source 70.Make nitrogen current 52 by humidifier jar 74, gas is heated to the water-bath of predetermined temperature via one by resistance heater 76 in jar, thereby desired steam is added in the gas.Adjusting by heater 76 electric currents makes humidifier 74 keep a certain predetermined water temperature, thereby makes supplemental air flow 52 keep predetermined water vapour content.
Valve 80 is being controlled the flow rate from the converted gas stream 50 of dry nitrogenous source 70.
In automaton 40, supervisory control comuter 90 with manual input device or keyboard 92 is connected to controller 100 by corresponding bidirectional data communication line 94, be used for reading out each sensor values of self-controller " truck ", set point and other data, and be used for sending set point to controller.Controller 100 comprises conventional distributed control module, and these control modules have the input that is connected to various sensor and are connected to the output of wide variety of equipment driver in the device for spinning, with monitoring operation and be spinning operation, automatic control is provided.Here only disclose those and be applied to the operation and the equipment of melt polymer relative viscosity control aspect automatically.
The input of each control module in the controller 100 is connected to following each sensor: promptly, the gas flow rate sensor 110 in the converted gas conduit 50,
Cooling-water temperature sensor 112 in the humidifier 74, gas flow rate sensor 114 in the make-up gas conduit 52, the gas temperature sensor 116 at recyclegas conduit 46 air inlet places 58, pressure sensor 118 in the exhaust manifolds 67, polymeric pressure sensor 120 at 26 beginnings of delivery catheter place, polymeric pressure sensor 122 in the manifold 28, polymer temperature sensor 124 in the manifold 28, and be connected on each sensor of monitoring operation and measuring pump 29 flow rates, to be used for monitoring corresponding flow rate, pressure and temperature.Each control module has the output that is connected on following each device in the controller 100: promptly, the valve operating system 130 of valve 80, control flows to the current control device (not shown) of the electric current of resistance heater 76, the valve operating system 134 of valve 72, the valve operating system 136 of valve 66, and the valve operating system 138 of valve 69, to flow and temperature according to corresponding each gas of each set point control in the controller 100.
Can or manually import the operation of (not shown) controller by various internal calculation, perhaps can come each set point the setting controller 100 by each signal of sending from supervisory control comuter 90.In this prior art system, three set points are by the relevant signal of viscosity Control being upgraded once in per 60 seconds with polymer phase from supervisory control comuter 90 is that send in the controller 100.These three set points controlled incessantly, that promptly once upgraded by described supervisory control comuter per minute are: (1) is based on the humidifier specific gas flow rate set point of being controlled humidifier flow rate valve 72 by 114 sensing flow rates of sensor, (2) based on the recyclegas temperature set-point of control valve 66 by 116 sensed temperature of sensor, and (3) compensates for differential pressure set point, use to calculate a converted gas flow rate set point, based on converted gas flow rate 80 being controlled by controller 100 by 110 sensing flow rates of sensor.Control heater 76 electric currents and do not upgrade of flowing through according to the temperature of reading autobiography sensor 112 according to the pressure of reading autobiography sensor 118 each set point to the control of air bleeding valve 69, and can only be in the artificial input change of normal operation period by the operator.Controller 100 is by being about 2H
zCycle frequency action, so controller calculated the signal of each device driver in per approximately 0.5 second and renewal once.
RV=((C
* 2T-C
3)
*(melt viscosity)
*C
4)+C
5()
Melt viscosity=(P
1-P
2)/(handling capacity
*C
1)
P
1=measuring from pressure sensor 120
P
2=measuring from pressure sensor 122
T=is from the polymer temperature of sensor 124
Handling capacity=from the handling capacity percentage of measuring pump 29
C
1=0.0001 to 0.0003(depends on geometric pipeline shape)
C
2＝0.882
C
3＝232
C
4＝0.3818
C
5=0.0 to 3.0(depends on ducted not extent of polymerization)
Equation (1) is measured according to the compensating for variations differential pressure in the polymer temperature, makes this result reflect the relative viscosity of melt polymer.
With reference to Fig. 3 B, in the step 178, uses common " three-mode " proportional-integral-differential (P-I-D) algorithm, with from step 152 Target Transformation specific gas flow rate, from the flow rate of converted gas at that time in step 160 and from the flow rate of make-up gas at that time in step 160 as independent variable, calculate a new make-up gas and flow set point.In the step 180, described new make-up gas stream set point is delivered to controller 100.Increase waste gas flowrate that the make-up gas flow rate causes higher moist recyclegas by exhaust outlet 67, thereby reduce the moisture percentage of recyclegas, and make polymer flake weaken depolymerization successively and increase the viscosity of melt polymer.Otherwise, reduce the make-up gas flow rate moisture percentage of recyclegas is improved, cause the viscosity of bigger depolymerization and melt polymer to lower.Thereby the set point of like this regulating make-up gas stream makes the converted gas flow rate keep approaching the Target Transformation specific gas flow rate.
The recyclegas that step 182,184,186,188 and 190 has then been determined to be used to that converted gas flow rate and make-up gas flow rate are remained on and has been scheduled within the bound scope is setovered.In step 182, converted gas stream is less than the lower limit of converted gas stream, and make-up gas stream causes transferring to the step 184 less than the lower limit of make-up gas stream in branch, be negative value with the recyclegas offset control there.If the step 182 is for being false, so program just enters the step 186, converted gas flows the upper limit greater than converted gas stream on this occasion, and make-up gas stream is greater than the upper limit of make-up gas stream, just cause in branch, transferring to the step 188, with the recyclegas offset control be there on the occasion of.If the step 186 for being false, goes on foot 190 so program enters, with the recyclegas offset control be there on the occasion of.If the step 186 for being false, so program enters the step 190, is zero with the recyclegas offset control there.
In the step 192 of Fig. 3 C, the biasing of setting in the step 184,188 or 190 of Fig. 3 B is added to recyclegas temperature set-point at that time, thereby produces a new recyclegas temperature set-point.In the step 198, will deliver to controller 100 from the new recyclegas temperature set-point in step 190.Reduce the recyclegas temperature and allow that polymer flake keeps more juicy in the container 44, converted gas stream is increased, conversion and make-up gas flow rate are remained on below the corresponding limit thereby can cause make-up gas stream to increase subsequently.Strengthen the recyclegas temperature and then reduce the thin slice moisture percentage, this has just increased the relative viscosity of polymer and has caused converted gas stream to reduce, thereby this forms make-up gas stream again successively and reduces to make conversion and make-up gas stream to remain on more than the corresponding lower limit.
Step 202 and 204, for controller 100 provides a new compensates for differential pressure set-point, this compensates for differential pressure set-point of controller 100 usefulness provided the primary control of converted gas stream in monitoring with computer.In the step 202, will be from step 150 target relative viscosity, be added to the P-I-D algorithm to calculate the compensates for differential pressure set-point of heat from the relative viscosity that calculates in step 162 with from the pressure of compensates for differential at that time in step 160.In the step 204, the compensates for differential pressure set-point that this is new is delivered to controller 100.
Fig. 4 illustrates the operation or the draft procedure of controller 100.In the step 210, this controller is read various sensors, such as sensor among Fig. 1 29,110,114,116,118,120,122 and 124, thereby obtains various at that time flow rates, temperature and pressure by these sensors monitored.In the step 216, read any new set point from supervisory computer 90, such as the set point that flows from the make-up gas that goes on foot 180, from the recyclegas temperature set-point in step 198, and from the compensates for differential pressure set-point that goes on foot 204.In the step 218, calculate compensates for differential pressure at that time according to following equation 2:
Delta-Pcom=(10 (P
1-P
2) * (0.1*y)+(2.85) (1-0.35*m)])/((0.286* handling capacity)) (2)
In the formula
Y is a polymer temperature 124 that record or at that time,
M is the subject polymer temperature, for example, and 290 ℃,
Y and M are write as 250 ℃ to 350 ℃ mark or the percentage in the scope for for the purpose of the adaptive controller algorithm pattern of the input,
P
1Be the pressure that sensor 120 is sensed
P
2Be the pressure that sensor 122 is sensed, and
The mark or the percentage of total spinning point or measuring pump 29 when handling capacity is operation.
In the step 224, controller 100 is used the P-I-D algorithms with from the compensates for differential pressure that calculates in the step 218, calculate a new converted gas flow rate set point from the compensates for differential pressure set-point in step 204 and 216 with from the flow rate of converted gas at that time in step 210 as independent variable.
In 228,230,232,234,236,238 and 240 each step, the control module that respectively distributes in the controller 100 is generally operated simultaneously with adjusting control valve 66,69, each driver signal of 72 and 80, and the electric current that passes through heater 76.In the step 228, read within the setting range of tolerable variance of the new settings the point whether stream of converted gas at that time that goes on foot 210 calculates in the step 224 through judgement.If be false, then program enters the step 230, thereby there signal is delivered to control valve device 130 control valves 80 to produce the channel gas flow rate of proofreading and correct; These signals provide incremental adjustments to be required the toning of gas stream to avoid.In the step 232, corresponding control module identifies that the flow rate of make-up gas at that time of reading autobiography sensor 114 is whether within the setting range of tolerable variance of set point, if be false then go on foot 234, signal is delivered to control valve device 124 with control valve 72 and make-up gas stream in this step.Conditioning period increment or time control provides delay to avoid the toning of make-up gas stream.In the step 236, if between the reading of temperature sensor 114 and the artificial set point of importing for the humidifier water temperature, there are differences, the flow through electric current of resistance heater 76 of corresponding control module increment ground adjusting.In the step 238, corresponding control module basis is in the recyclegas temperature of 116 sensings of sensor and any difference between the recyclegas temperature set-point, and increment ground control valve 66 passes through the steam flow rate of heater 64 to improve or to reduce the recyclegas temperature with adjusting.In the step 240, corresponding control module is regulated air bleeding valve 69 according to any difference between the recyclegas pressure set-point of 118 pressure sensors of sensor and artificial input, increment ground.
In the step 242, controller 100 is delivered to controller " truck " so that supervisory control comuter 90 can be read with each sensor reading and calculated value.Controller 100 just can begin a new operation cycle then.
The prior art system of Fig. 1-4 provides the control of desirable polymer relative viscosity for single screw rod extruding device, but when system applies is arrived the twin-screw extruding device, just find that this system can produce bigger change on the relative viscosity of melt polymer.This causes the excessive variation of spun filament aspect toughness, percentage elongation and dyeability.
The present invention can be summarised as process and the equipment that is used for the spinning of synthesizing linear polyamide, wherein take humidifier water temperature and converted gas stream to regulate simultaneously first control is provided with relative viscosity to molten polyamide.The adjusting of described primary control or humidifier water temperature and converted gas stream is based on the difference between the molten polyamide relative viscosity of carrying out spinning of being scheduled to relative viscosity and recording.
In one embodiment, thus make the polyamide thin slice in succession by first and second container handlings fusings.Before making it to form long fiber, the polyamide that squeezes out fusing via spinneret determines the relative viscosity of molten polyamide.First handles gas by first container handling.Flow rate and the adjusting of moisture percentage and the humidity that first adjustment of handling gas has changed the first processing gas by means of make-up gas stream.The second processing gas is dry, and it is by second container handling.The moisture percentage of make-up gas stream and second flow rate of handling gas correspondingly are directly proportional according to measured molten polyamide relative viscosity or regulate inversely to keep a desired relative viscosity.
The objective of the invention is provides a kind of method and apparatus for the synthesizing linear polyamide is spun into long fiber, and the long fiber that is spun into the present invention all is being significantly improved aspect toughness, percentage elongation and the dyeability uniformity.
An advantage of the invention is the moisture percentage and the converted gas flow rate of regulating make-up gas stream simultaneously, thereby the uniformity of polymer performance is improved according to the difference that exists between relative viscosity that records and target relative viscosity.
A feature of the present invention is by the adjusting of converted gas stream and the make-up gas water capacity primary control to relative viscosity, with the deputy control of regulating by make-up gas stream, and the tertiary control of regulating by recyclegas takes place simultaneously.Difference between the adjusting of described deputy control or make-up gas stream is flowed based on intended conversion gas stream and the converted gas that records.The adjusting of tertiary control or recyclegas temperature exceeds desired scope based on make-up gas stream and converted gas stream.
To most preferred embodiment and the description of the drawings, will be more clear and definite to other purposes of the present invention, advantage and feature from following.
Fig. 1 is that prior art is used for the equipment of polyamide spinning and the sketch of process.
Fig. 2 is that the monitoring of Fig. 1 is with the flow chart that the related parameter input process is arranged in the prior art program in the computer.
Fig. 3 A is the flow chart that supervisory control comuter is used for the prior art control program first of whole control in the equipment of Fig. 1 and the method.
Fig. 3 B is the equipment of Fig. 1 and the flow chart that the method supervisory control comuter is used for the prior art control program second portion of whole control.
Fig. 3 C is the equipment of Fig. 1 and the flow chart that the method supervisory control comuter is used for the prior art control program third part of whole control.
Fig. 4 is the flow chart of prior art program that is used for the controller of application drawing 1.
Fig. 5 is the sketch that is used for polyamide spinning equipment and method that the present invention proposes.
Fig. 6 is that each program step is used with the flow chart of monitoring in pie graph 5 equipment and the method with the add-in program step of the control program of computer in Fig. 3 A, 3B and 3D.
Fig. 7 be used for replacing a program step among Fig. 4 be configured for application drawing 5 middle controllers through improved program step.
As illustrated among Fig. 5,6 and 7, the present invention is used for equipment and the method that twin-screw squeezer 300 is used in the polyamide spinning, be included in the step 310,312 and 314 in supervisory control comuter 90 control programs, and be included in controller 100 programs through the improved step 236 ', the step 236 ' be used for according to molten polyamide relevant through what determine Viscosity changes the moisture percentage of make-up gas stream 52 with the difference of selected relevant viscosity. This primary humidity control is simultaneous with the flow rate variation of converted gas stream 50. Therefore, Fig. 5,6 and 7 equipment and method first control having simultaneous polymer relative viscosity by the variation that contains water content of converted gas flow rate and make-up gas. Have been found that first control of this double base compares with first control of unicity that only changes converted gas stream in double helix equipment and method, reduce significantly the variation from the melt polymer relative viscosity aspect of twin-screw squeezer.
The equivalent elements that equipment shown in Fig. 5 and Fig. 1 equipment have a similar 26S Proteasome Structure and Function is used same numeral in the application drawing 1 all. Increase by a booster 82 output of screw melter 300 is connected to delivery catheter 26. The position of melt polymer temperature sensor 124 is moved on to delivery catheter 26 from manifold 28. In addition, article one, dotted line represents optionally booster 82 not to be linked controller 100, in order to use throughput is measured in the speed measurement of booster 82 with the another kind that replaces prior art to pass through the sensor measurement throughput rates on measuring pump 29 as throughput rates mode.
The program step 310,312 and 314 of Fig. 6 is added in the program of Fig. 3 A, 3B and 3C, with the control program in pie graph 5 supervisory control comuters 90. In the step 310, supervisory computer 90 reads out the at that time humidifier water temperature of self-controller 100. By making it to comprise the step 310 to steps 160 correct of Fig. 3 A and the data that read out on the controller " truck ". At next step in 312, use conventional proportional-integral-differential (P-I-D) algorithm, with the target relative viscosity from the step 150, input in the algorithm as independent variable from the relative viscosity that calculates in step 162 with from the at that time humidifier temperature that goes on foot 310, calculate a new humidifier temperature set-point by computer 90. In the step 314, this new humidification actuator temperature set point is delivered to controller 100 then.
In the director demon of Fig. 5 controller 100, the step 236 of the program step 236 of Fig. 7 ' replacement Fig. 4. Controller 100 reads out the humidifier temperature set-point from supervisory control comuter 90 in the step 216 of Fig. 4, then this set point is used for Fig. 7 through the improved step 236 ', with the adjusting electric current of heater 76 of flowing through, thereby change the humidifier temperature. Because the change of the relative viscosity that the set point of humidifier temperature is basis in the step 312 to be calculated changes, so the humidifier temperature also changes along with the change of the relative viscosity that calculates. When the relative viscosity that calculates or record increased, the humidifier temperature also improved thereupon, thereby formed that moisture percentage increases and the enhancing of Depolymerisation of polyamides effect and make the relative viscosity decline of melt polymer. Otherwise when the relative viscosity that records descended, the humidifier temperature also descended thereupon, thereby caused relative viscosity to increase also reducing aspect the thin slice moisture percentage.
When the adjusting of humidifier temperature or make-up gas water content is taken place simultaneously as first control and adjusting as the converted gas flow rate of first control, experiment has proved that the control of relative viscosity is improved significantly. This be considered to have more than in the improvement aspect the uniformity of relative viscosity be limited to the twin-screw spinning equipment, also can be applicable to other and resemble in the spinning process the single screw spinning method.
By the conclusion that experience draws, namely change converted gas stream four kinds of parameters of controlling the polymer relative viscosities are had the most rapidly reaction. For example, for relative viscosity is at that time changed at that time (1-e ') value of relative viscosity, each time constant during such as each control parameter independent role is: be 10 minutes for the converted gas flow rate; Being 45 minutes for the make-up gas flow rate, is 60 minutes for the humidifier temperature, then is 120 minutes for the recyclegas temperature.
Example
In one example, according to the used control element of the equipment of Fig. 5 as list at table 1 and program thereby shown in Fig. 2,3A, 3B, 3C, 4,6 and 7.In supervisory control comuter 90 programs, go on foot 178,202 and 312 " Instrument Engineers ' Handbook(Process Control) " book chapter 1,1,2 of having used that Chiltor Book Co of Randnor publishes, B.G.Liptak edit and save described P-I-D algorithm.Use Honeywell in the controller 100 and expand controller algorithm 24, multiplication/division, (Honeywell reference manual 25-220) carries out programming to going on foot 218 equation (2).Used P-I-D algorithm is a Honeywell algorithm 01 in the step 224, Honeywell reference manual 25-220.
Table 1
Supervisory control comuter 90 DEC VAX 8200
Digital Equip
Corp，Maynard，MA
Local control 100,102,104, Honeywell
Be used for converted gas stream, 106 and 108 TDC/2000
The humidifier temperature, Honeywell Inc.,
Make-up gas stream, Industrial
Recyclegas temperature and Controls
Relative viscosity is measured Division
Gas flowmeter 110,114 Honeywell ST3000
Smart
Transmitter
Polyalcohol pressure 132,134 Honeywell ST3000
Sensor bulb Smart
Transmitter
The melt-extruded device 24 Werner ﹠amp of spiral;
Pfleiderer
zsk120 extruder
With transmitter type JJ;
Moore
Industries Model
433774
Having the standard moisture absorption rate is that 0.2% nylon 6,6 polymer flakes feed the thin slice adjuster 20 shown in Fig. 5.Target relative viscosity in 53 to 72 scopes and the Target Transformation specific gas flow rate selected by following scope are manually to input to supervisory control comuter 90.Under whole spinning point service conditions, polymer temperature is controlled in the 280-290 ℃ of scope, and handling capacity is 1700-2000 pound (770-910kgm) per hour.Each set point in four controllers is remained within the following scope of listing:
The converted gas flow rate ... the 0-6 cubic feet/minute (the 0-0.17 cubic meter/minute)
The make-up gas flow rate ... the 15-45 cubic feet/minute (the 0.4-1.3 cubic meter/minute)
The humidifier temperature ... 30-45 ℃
The recyclegas temperature ... 155-190 ℃
Because under scope and spirit of the present invention, can make many detailed modification, variation and change to the foregoing description, therefore need above description of explanation and accompanying drawing only should be interpreted as illustrative and there is no limited significance.
Claims (19)
1, a kind of method that is used for the synthesizing linear polyamide is carried out spinning, it comprises:
The polyamide thin slice is passed through first and second container handlings by easy stages,
Make a kind of inertia heated air cycle through polyamide thin slice in first container handling,
The inert gas that makes a kind of drying with variable flow rate by the polyamide thin slice in second container handling,
Make a kind of make-up gas stream be added to the circulation heated air controlling the moisture percentage of this circulation heated air with variable moisture percentage,
The molten polyamide thin slice,
Determine the relative viscosity of molten polyamide,
Change the moisture content of dry inert gas flow rate and make-up gas simultaneously according to the relative viscosity of determined molten polyamide, thereby make molten polyamide keep selected relative viscosity, and
Molten polyamide is pressed through spinneret to form long fiber.
2, a kind of method as claimed in claim 1, it is characterized in that determining that relative viscosity comprises: the differential pressure between delivery catheter two ends of measurement melt polymer, measure the temperature of melt polymer, determine the handling capacity of melt polymer, and calculate relative viscosity according to the differential pressure of gained, comprising according to a certain predetermined temperature being any variation of polymer temperature and the differential pressure that records is compensated and is any variation of handling capacity and the differential pressure that records is compensated according to a certain predetermined throughput.
3, a kind of method that is used for the synthesizing linear polyamide is carried out spinning as claimed in claim 2 also comprises: thereby be higher or lower than the flow rate that a certain predeterminated target flow rate changes make-up gas according to the dry inert gas flow rate dry gas flow rate is kept near the target flow rate, thereby and be higher or lower than the temperature that the corresponding predetermined upper limit and lower limit change the circulation heated air according to the flow rate of dry inert gas and make-up gas the flow rate of dry inert gas and make-up gas is remained within the effective range.
4, a kind of method as claimed in claim 1 is characterized in that by the moisture content that make-up gas stream is changed make-up gas by water-bath and the temperature that changes water-bath.
5, a kind of method as claimed in claim 2 is characterized in that by the moisture content that make-up gas stream is changed make-up gas by water-bath and the temperature that changes water-bath.
6, a kind of method as claimed in claim 3 is characterized in that by the moisture content that make-up gas stream is changed make-up gas by water-bath and the temperature that changes water-bath.
7, a kind of method as claimed in claim 4, it is characterized in that the relative viscosity determining and select according to the P-I-D algorithm application and at that time water temperature change the temperature of water-bath as the input of giving algorithm.
8, a kind of method as claimed in claim 5, it is characterized in that the relative viscosity determining and select according to the P-I-D algorithm application and at that time water temperature change the temperature of water-bath as the input of giving algorithm.
9, a kind of method as claimed in claim 6, it is characterized in that the relative viscosity determining and select according to the P-I-D algorithm application and at that time water temperature change the temperature of water-bath as the input of giving algorithm.
10, a kind of equipment that is used for the synthesizing linear polyamide is carried out spinning, it comprises:
Pass through the first and second continuous container handlings of usefulness therebetween for the polyamide thin slice.
Be used for making a kind of inertia heated air to cycle through the device of polyamide thin slice in first container handling,
The inert gas that is used for making a kind of drying is with the device of variable flow rate by polyamide thin slice in second container handling,
Be used for making a kind of make-up gas stream to be added to the circulation heated air controlling the device of this circulation heated air moisture percentage with variable moisture percentage,
Be connected to and be used for receiving the also melter of molten polyamide thin slice on second container handling,
Be used for determining the device of molten polyamide relative viscosity,
Thereby according to the relative viscosity of determined molten polyamide, be used for changing simultaneously dry inert gas flow rate and make-up gas moisture content and make molten polyamide keep the device of selected relative viscosity, and
Be used for accepting molten polyamide from melter to form long stapled spinneret.
11, a kind of equipment as claimed in claim 10, it is characterized in that being used for determining that the device of relative viscosity comprises: a delivery catheter, be used for measuring the device of differential pressure between delivery catheter two ends of melt polymer, be used for measuring the device of melt polymer temperature, be used for determining the device of melt polymer handling capacity, and be used for calculating the device of relative viscosity according to measured differential pressure, be used for the differential pressure that records is compensated and is any variation of handling capacity and device that the differential pressure that records is compensated according to a certain predetermined throughput comprising any variation that according to a certain predetermined temperature is polymer temperature.
12, a kind of equipment that is used for the synthesizing linear polyamide is carried out spinning as claimed in claim 11 also comprises: make the dry gas flow rate keep device near the target flow rate thereby be higher or lower than flow rate that a certain predeterminated target flow rate is used for changing make-up gas according to the dry inert gas flow rate, thereby and be higher or lower than temperature that the corresponding predetermined upper limit and lower limit be used for changing the circulation heated air according to the flow rate of dry inert gas and make-up gas and make the flow rate of dry inert gas and make-up gas remain on device within the effective range.
13, a kind of equipment as claimed in claim 10, the device that it is characterized in that being used for changing the make-up gas moisture content comprises: a water bath, be used for making make-up gas to pass through the device of this water bath, and the device that is used for changing the water bath temperature.
14, a kind of equipment as claimed in claim 11, the device that it is characterized in that being used for changing the make-up gas moisture content comprises: a water bath, be used for making make-up gas to pass through the device of this water bath, and the device that is used for changing the water bath temperature.
15, a kind of equipment as claimed in claim 12, the device that it is characterized in that being used for changing the make-up gas moisture content comprises: a water bath, be used for making make-up gas to pass through the device of this water bath, and the device that is used for changing the water bath temperature.
16, a kind of equipment as claimed in claim 13, the device that it is characterized in that being used for changing the water bath temperature comprise that using a relative viscosity that the P-I-D algorithm determines and select with institute reaches water temperature at that time as the computer installation to the input of algorithm.
17, a kind of equipment as claimed in claim 14, the device that it is characterized in that being used for changing the water bath temperature comprise that using a relative viscosity that the P-I-D algorithm determines and select with institute reaches water temperature at that time as the computer installation to the input of algorithm.
18, a kind of equipment as claimed in claim 15, the device that it is characterized in that being used for changing the water bath temperature comprise that using a relative viscosity that the P-I-D algorithm determines and select with institute reaches water temperature at that time as the computer installation to the input of algorithm.
19, a kind of equipment as claimed in claim 10 is characterized in that melter comprises a double helix melter.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US07/308,773 US4952345A (en) | 1989-02-10 | 1989-02-10 | Method for controlling polymer viscosity |
| US308,773 | 1989-02-10 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1045137A true CN1045137A (en) | 1990-09-05 |
Family
ID=23195340
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN90100682A Pending CN1045137A (en) | 1989-02-10 | 1990-02-10 | Controlling polymers method of viscosity and equipment |
Country Status (8)
| Country | Link |
|---|---|
| US (1) | US4952345A (en) |
| EP (1) | EP0382569A3 (en) |
| JP (1) | JPH02242911A (en) |
| KR (1) | KR900013112A (en) |
| CN (1) | CN1045137A (en) |
| AU (1) | AU615869B2 (en) |
| BR (1) | BR9000594A (en) |
| CA (1) | CA2009524A1 (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1047414C (en) * | 1995-06-07 | 1999-12-15 | 刘兆峰 | Ultrastrength polyethylene fibre spinning apparatus |
| CN1312333C (en) * | 2000-08-29 | 2007-04-25 | 比勒股份公司 | Method for melting a polymer granulate and melt element |
| CN101498056B (en) * | 2009-02-04 | 2010-12-08 | 浙江华欣新材料股份有限公司 | Equipment and method for melt direct spinning online multicomponent adding production color and functional fibre |
| CN112981560A (en) * | 2021-03-09 | 2021-06-18 | 邵阳学院 | Electrostatic spinning device capable of adjusting viscosity of polymer solution |
Families Citing this family (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CH688554A5 (en) * | 1994-03-22 | 1997-11-14 | Rhone Poulenc Filtec Ag | Industrial PA 6.6 filaments |
| US5955569A (en) * | 1996-11-27 | 1999-09-21 | E.I. Du Pont De Nemours And Company | Method for solid phase polymerization |
| KR100514570B1 (en) | 1997-05-29 | 2005-09-15 | 이 아이 듀폰 디 네모아 앤드 캄파니 | Process Control Method for Vented Polymerizers |
| US6235390B1 (en) | 1998-11-03 | 2001-05-22 | E. I. Du Pont De Nemours And Company | High RV filaments, and apparatus and processes for making high RV flake and the filaments |
| GB0018162D0 (en) * | 2000-07-26 | 2000-09-13 | Dow Corning Sa | Polymerisation reactor and process |
| DE60315314T2 (en) * | 2002-09-16 | 2008-05-08 | Invista Technologies S.A.R.L., Wilmington | PREPARATION OF POLYAMIDE YARN AND POLYAMIDE YARN |
| KR101421192B1 (en) * | 2013-03-04 | 2014-07-23 | 주로테크 주식회사 | Screw cooling device for transfering powder of screw conveyor |
| NO339255B1 (en) * | 2013-05-22 | 2016-11-21 | Multivector As | Apparatus for swirling at least one fragmented substance |
| ITUB20159282A1 (en) | 2015-12-18 | 2017-06-18 | Piovan Spa | METHOD AND SYSTEM OF CONTROL OF A DEHUMIDIFICATION AND / OR DRYING SYSTEM |
| US10309901B2 (en) * | 2017-02-17 | 2019-06-04 | International Business Machines Corporation | Water-sensitive fluorophores for moisture content evaluation in hygroscopic polymers |
| MX2021007383A (en) | 2018-12-18 | 2021-09-23 | Ascend Performance Mat Operations Llc | Antimicrobial polymer compositions, fibers, and yarns. |
Family Cites Families (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2571975A (en) * | 1947-05-10 | 1951-10-16 | Du Pont | Melt spinning process |
| NL97740C (en) * | 1957-03-08 | |||
| DD129239B1 (en) * | 1976-11-12 | 1981-01-28 | Loichen Hans Dieter | capillary |
| EP0092898B2 (en) * | 1982-04-28 | 2000-02-09 | E.I. Du Pont De Nemours And Company | Process for remelting polyamides |
| US4721589A (en) * | 1983-09-22 | 1988-01-26 | Harrel, Inc. | Extruder viscosity control system and method |
| US4721448A (en) * | 1985-12-19 | 1988-01-26 | Adolph Coors Company | Pelletizer with moisture control system |
-
1989
- 1989-02-10 US US07/308,773 patent/US4952345A/en not_active Expired - Lifetime
-
1990
- 1990-02-07 CA CA002009524A patent/CA2009524A1/en not_active Abandoned
- 1990-02-09 JP JP2028654A patent/JPH02242911A/en active Pending
- 1990-02-09 KR KR1019900001568A patent/KR900013112A/en not_active Application Discontinuation
- 1990-02-09 EP EP19900301417 patent/EP0382569A3/en not_active Withdrawn
- 1990-02-09 BR BR909000594A patent/BR9000594A/en not_active Application Discontinuation
- 1990-02-09 AU AU49277/90A patent/AU615869B2/en not_active Ceased
- 1990-02-10 CN CN90100682A patent/CN1045137A/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1047414C (en) * | 1995-06-07 | 1999-12-15 | 刘兆峰 | Ultrastrength polyethylene fibre spinning apparatus |
| CN1312333C (en) * | 2000-08-29 | 2007-04-25 | 比勒股份公司 | Method for melting a polymer granulate and melt element |
| CN101498056B (en) * | 2009-02-04 | 2010-12-08 | 浙江华欣新材料股份有限公司 | Equipment and method for melt direct spinning online multicomponent adding production color and functional fibre |
| CN112981560A (en) * | 2021-03-09 | 2021-06-18 | 邵阳学院 | Electrostatic spinning device capable of adjusting viscosity of polymer solution |
| CN112981560B (en) * | 2021-03-09 | 2022-07-29 | 邵阳学院 | Electrostatic spinning device capable of adjusting viscosity of polymer solution |
Also Published As
| Publication number | Publication date |
|---|---|
| AU615869B2 (en) | 1991-10-10 |
| KR900013112A (en) | 1990-09-03 |
| EP0382569A3 (en) | 1991-11-06 |
| BR9000594A (en) | 1991-01-15 |
| JPH02242911A (en) | 1990-09-27 |
| CA2009524A1 (en) | 1990-08-10 |
| EP0382569A2 (en) | 1990-08-16 |
| AU4927790A (en) | 1990-08-16 |
| US4952345A (en) | 1990-08-28 |
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